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WO1997016505A1 - Procede de recuperation de propane - Google Patents

Procede de recuperation de propane Download PDF

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Publication number
WO1997016505A1
WO1997016505A1 PCT/IB1996/001249 IB9601249W WO9716505A1 WO 1997016505 A1 WO1997016505 A1 WO 1997016505A1 IB 9601249 W IB9601249 W IB 9601249W WO 9716505 A1 WO9716505 A1 WO 9716505A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas stream
stream
absorber
separator
propane
Prior art date
Application number
PCT/IB1996/001249
Other languages
English (en)
Inventor
James N. Sorensen
Original Assignee
Mcdermott Engineers & Constructors (Canada) Ltd.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Mcdermott Engineers & Constructors (Canada) Ltd. filed Critical Mcdermott Engineers & Constructors (Canada) Ltd.
Priority to GB9807591A priority Critical patent/GB2323605B/en
Priority to CA002235883A priority patent/CA2235883C/fr
Priority to AU73296/96A priority patent/AU7329696A/en
Publication of WO1997016505A1 publication Critical patent/WO1997016505A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1418—Recovery of products
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/04—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with liquid absorbents
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/08—Processes or apparatus using separation by rectification in a triple pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop

Definitions

  • This invention pertains to a system and a process for recovering propane, butane and heavier hydrocarbon components from natural gas thereby also generating a gas stream consisting primarily of methane and ethane.
  • U.S. Patent Nos. 4,854,955, 4,869,740, 4,889,545, and 5,275,005 to Campbell et al disclose the step of expanding a vapor received from a separator prior to delivering same to a distillation column.
  • U.S. Patent Nos. 4,507,133 and 4,617,039 each disclose a step of expanding a vapor received from a separator and contacting same in an absorber with absorbed components delivered to a distillation column.
  • U.S. Patent No. 5,325,673 to Durr et al discloses a method of pre-treating a natural gas stream using a single scrub column in order to remove freezable C 5 ⁇ components.
  • This method consists of feeding a natural gas stream to a feed point on a scrub column operated substantially as an absorption column wherein the heavy components are absorbed from the feed gas using a liquid reflux that is essentially free of such C s . components.
  • the reflux stream can be overhead vapor condensate having a temperature of about -40°C, or methane-rich liquified natural gas (LNG) or a combination of LNG and vapor condensate.
  • a further object of this invention is to pump cryogenic hydrocarbon liquid from a downstream separator that is coupled to the expander outlet of the compressor/expander.
  • This pump delivers the hydrocarbon liquid either directly or through a heat exchanger and then recycles it back to the upstream absorber.
  • Yet another object of this invention is to deliver the gas leaving the upper region of the distillation column to a heat exchanger. In one variation of the process, this heat exchanger cools and partially condenses said gas which then flows to and joins the feed to the separator that is coupled to the expander outlet .
  • a portion of the process feed gas is chilled using the gas from the overhead of the distillation column (which may or may not be mixed with the overhead of the separator which is downstream of the expander) , this portion of the chilled feed gas is then used to cool the overhead gas stream from the distillation tower and the heat so acquired is then used to reboil the bottom of the absorber.
  • An improvement is described to a process for recovering propane and other heavier components from a natural gas stream.
  • This process incorporates the step of locating a separator downstream of a turbo-expander and removing a liquid stream from the separator.
  • This liquid stream removed from the separator is then returned and injected into an upper region of the upstream absorber.
  • this liquid stream absorbs propane and heavier hydrocarbon compounds from the natural gas stream fed into the absorber.
  • a methane and ethane rich gas stream is then removed from the downstream separator while a stream rich in propane, butane, and other heavy hydrocarbon components of the natural gas stream is removed from the bottom of the absorber and routed to the distillation column for separation of the light and heavy components .
  • Fig. 1 is a schematic diagram of the system and process (10) disclosed herein. While parts of this schematic are well known in the art, the interconnections and arrangement of the absorber, expander, separator and distillation column comprise the core of this invention.
  • Fig. 2 is a schematic diagram of an alternate system and process (70) .
  • Fig. 3 is yet another schematic diagram of a further alternate system and process (110) .
  • Natural gas (12) feed is injected into a lower region of absorber (14) after being chilled in heat exchangers (16) and (18) .
  • absorber (14) As the chilled and partially condensed feed gas (12) passes through absorber (14) , the gaseous portion thereof flows upward through a packed section or other contacting device such as a trayed section, while the liquid portion thereof flows downward. Discharged from absorber (14) is bottom liquid stream (20) and upper gas stream (22) .
  • bottom liquid stream (20) flows directly to an upper region of distillation column or deethanizer (24) via line (26) and a portion of this bottom liquid stream (20) from absorber (14) is warmed in heat exchanger (18) and then delivered to a more central region of distillation column or deethanizer (24) via line (28) .
  • the split may vary from all to line (26) to all line (28) .
  • Upper gas stream (22) exiting absorber (14) is then delivered to expander (30) of a compressor/expander.
  • the ensuing expansion of gas stream (22) liquifies a portion of it with the resultant liquid-gas stream (32) exiting expander
  • separator (34) It is within separator (34) that the incoming liquid-gas stream (32) is separated into upper gas stream (36) and lower liquid stream (38) .
  • upper gas stream (36) is then cross-exchanged with incoming natural feed gas (12) in heat exchanger (16) . The effect is to chill stream (12) while warming stream (36) .
  • Subsequent heat exchange or warming of gas stream (36) in heat exchanger (40) is achieved after which gas stream (36) from separator (34) enters the compressor side (42) of the compressor/expander.
  • the now pressurized gas stream may then be further compressed and cooled, if so desired, before the resulting residue gas (44) , consisting primarily of methane and ethane, is delivered elsewhere.
  • this stream is pumped via pump (46) to heat exchanger (48) for warming before being delivered or recycled back to absorber (14) via line (50) .
  • this bottom liquid stream (38) would be sent directly to distillation column (24) ,- however, in process
  • liquid stream (38) is instead warmed and partially vaporized in heat exchanger (48) and returned to absorber (14) .
  • This warmed and partially vaporized liquid stream (50) separates from the vapor at the top of absorber (14) , and then flows downward in absorber (14) .
  • the liquid from stream (50) absorbs more of the propane and heavier components in the gas entering the absorber and less of the ethane and lighter components which remain in their gaseous state for discharge via gas stream (22) .
  • distillation column or deethanizer (24) upper gas stream (52) is discharged therefrom and sent to heat exchanger (48) for cooling via cross-exchange with cold liquid stream (38) from separator (34) .
  • This now cooled gas stream (52) is then delivered and mixed with liquid/gas stream (32) before this stream (32) enters separator (34) .
  • This recycle of gas stream (52) from distillation column (24) aids or improves the recovery of hydrocarbons in process (10) .
  • the duty of heat exchanger (48) is maximized consistent with economical temperature approaches.
  • Bottoms product liquid stream (54) from distillation column (24) which consists primarily of propane, and other heavier components, is also cooled as shown and delivered elsewhere for further processing and/or use.
  • some of the pertinent features of this process (10) include pump (46) which pumps cryogenic hydrocarbon liquid (38) from separator (34) that is coupled to the outlet of expander (30) .
  • This liquid stream (38) is delivered to absorber (14) , located upstream of expander (30) , but generally after being warmed in heat exchanger (48) .
  • heat exchanger (48) By warming liquid stream (38) in heat exchanger (48) , a hydrocarbon two-phase stream is generated that travels through line (50) before being injected at or near the top of absorber (14) .
  • the vapor portion of two-phase stream (50) that is injected into absorber (14) adds to the vapor leaving absorber (14) in upper gas stream (22) .
  • This upper gas stream (22) then enters expander side (30) of an expander/compressor.
  • Such extra vapor now passing through expander (30) increases the refrigeration effect of process (10) since additional work is done by the increased quantity of expanding gas.
  • more power is now supplied to compressor side (42) of the expander/compressor which is used to compress methane and ethane rich gas stream (36) .
  • Absorber (14) may comprise any number of theoretical stages. It may consist of phase separation of stream (12) followed by one or more contacting stages or it may be just a separator in which case stream (50) is optimally combined with stream (12) before entering the separator.
  • stream (20) is split first and then let down in pressure via separate control valves passing streams (26) and (28) .
  • a typical example of process (10) would be as follows (with the specified temperatures (°F) and pressures (psia) only being approximations) .
  • Natural feed gas (12) enters process (10) at a temperature of 80°F and a pressure of 580 psia. After appropriate portions of gas pass through heat exchanger (16) and (18) , the resultant temperature and pressure of feed gas (12) are about -93°F and 575 psia. It is at these values that gas stream (12) enters absorber (14) .
  • Bottom liquid product (20) and upper gas stream (22) exiting absorber (14) are also at about the same temperature and pressure as incoming gas (12) however their compositions are significantly different.
  • Upper gas stream (22) remains methane and ethane rich, but its concentrations of propane, butane and other heavier components are significantly reduced.
  • bottom liquid product (20) still contains some relatively small concentrations of methane and ethane, but it also contains all or nearly all of the propane, butane and heavier components originally found in natural feed gas stream (12) .
  • Upper gas stream (22) leaving absorber (14) is at about
  • separator (32) is at a temperature of about -116°F and a pressure of 384 psia.
  • gas stream (52) from deethanizer (24) Upon mixing with gas stream (52) from deethanizer (24) , the resulting stream entering separator (34) is at a temperature of about -113°F and a pressure of about 382 psia.
  • the combined streams (i.e. (32) and (52)) remain very methane and ethane rich while containing relatively low, if insignificant, quantities of propane, butane and the like.
  • Exiting separator (34) are methane and ethane rich gas stream (36) and propane rich liquid stream (38) at similar temperatures and pressures.
  • Methane and ethane rich gas stream (36) is then used to cool incoming natural feed gas (12) via heat exchanger (16) .
  • gas stream (36) is at a temperature of about 71°F and 377 psia.
  • Subsequent warming in heat exchanger (40) generates a stream at about 101°F and 372 psia. It is at this temperature and pressure that gas stream (36) enters compressor (42) .
  • stream (36) continues to contain predominantly methane and ethane and only small to insignificant quantities of propane, butane and the like at a temperature of about 119°F and at a pressure of 414 psia.
  • the resulting bottom liquid stream (20) is at a temperature of about -94°F and a pressure of about 575 psia.
  • the bottom liquid stream (20) now contains even greater concentrations of propane and heavier components.
  • bottom liquid stream (20) Upon being flashed across valve (56) , bottom liquid stream (20) is at a temperature of about -113°F and a pressure of about 401 psia. A portion of this stream is sent via line
  • the ethane and lighter components are stripped from the incoming streams (26) and (28) and discharged via upper gas stream (52) .
  • the propane and heavier components are discharged via bottoms product (54) .
  • This bottoms product (54) contains none to insignificant quantities of ethane and methane therein.
  • upper methane and ethane rich gas stream (52) contains small to insignificant quantities of propane, butane and the like therein.
  • Upper methane and ethane rich gas stream (52) leaves deethanizer (24) at a temperature of about -37°F and at a pressure of about 387 psia. After being cooled by cross- exchange with liquid stream (38) from separator (34) in heat exchanger or deethanizer overhead condenser (48) , its temperature is reduced to about -96°F. Upon such cooling, this methane and ethane rich stream (52) is combined with liquid-gas stream (32) for delivery to separator (34) so that separation of the lighter components (methane and ethane) from the heavier components (propane, butane, pentane, hexane and the like) are accomplished as previously described.
  • Propane and butane rich bottoms product (54) leaves deethanizer (24) at a temperature of about 192°F and a pressure of about 392 psi.
  • This bottoms product stream (54) is cooled in air cooler (62) to a temperature of about 109°F. Afterwards, this propane and butane rich stream (54) is sent elsewhere for processing.
  • Fig. 2 there is shown a schematic diagram of an alternate system and process according to the present invention. Like numerals designate like or similar features throughout the several views.
  • the alternate system and process (70) is quite similar to process (10) shown in Fig. l.
  • the advantages of the alternate process (70) are greater flexibility in design and greater propane recovery for the same compression horsepower.
  • the recovery of propane will be generally greater than 95% using process (70) .
  • a reboiled absorber (72) is used instead of absorber
  • a reboiler (74) strips out a large portion of the methane and ethane that would otherwise enter the deethanizer (24) so that the deethanizer does not have to fractionate so hard.
  • the reboiler (74) in this design also serves as an overhead reflux condenser for the deethanizer.
  • the reboiler (74) provides stripping vapor in stream (76) to the bottom of the absorber (72) .
  • Another feature of this design is a cold feed stream (78) to the absorber (72) which is developed by cooling it by heat exchange with expander (30) outlet vapors in heat exchanger (84) .
  • This alternate process (70) is only slightly more complex than process (10) with one additional exchanger (84) , one additional vessel (86) , and one additional pump (92) .
  • natural gas feed (12) is split into two portions (82) and (86) .
  • Stream (86) is cooled in heat exchanger (18) .
  • Stream (82) is further split into streams (76) , (78) and (80) which are cooled in heat exchanger (16A) .
  • Portion (78) is further cooled in heat exchanger (84) as described earlier and injected into a mid-region of absorber (72) .
  • Portion (80) is directly introduced into the absorber (72) in a slightly lower stage or tray.
  • the third portion (76) passes through reboiler (74) where it is used to cool and partially condense deethanizer (24) outlet vapor stream (52) , and then stream (76) is introduced into the lower region of absorber (72) .
  • the cooled feed stream (86) is also directly introduced in the lower region of absorber (72) at a temperature less than the third portion (76) .
  • Bottom liquid stream (20) flows through valve (56) to lower the pressure and temperature and is warmed in heat exchanger (18) before being delivered to a central region of the distillation column or deethanizer (24) via line (28) .
  • deethanizer (24) is shown smaller in size in Figs. 2 and 3, it is understood that it is identical in structure and function to that shown in Fig. 1 as the like numeral (24) indicates.
  • upper gas stream (52) which is methane and ethane rich is discharged and passed through reboiler (74) .
  • Reboiler (74) causes a large portion of the methane and ethane to be stripped from the feed to absorber
  • Reboiler (74) also serves as an overhead reflux condenser for deethanizer (24) .
  • the upper gas stream (52) passes through reboiler (74) and enters reflux separator (86) .
  • Bottom product liquid stream (54) from deethanizer (24) which consists primarily of propane, butane, pentane and other heavy hydrocarbons, may be cooled with optional cooler (62) (as shown in Fig. 1) .
  • optional cooler (62) as shown in Fig. 1.
  • the lower liquid stream (90) is sent via pump (92) through level control valve (94) back into the upper region of deethanizer (24) for fractionation.
  • Stream (22) remains methane and ethane rich with concentrations of propane, butane and other heavier components significantly reduced.
  • Stream (22) is discharged from absorber (72) and passes through an expansion means like turbo-expander (30) of compressor (42) /expander (30) which are preferably serially connected.
  • the liquid/gas stream (32) exiting expander (30) enters reflux separator (96) where liquid/gas stream (32) is separated into an upper methane and ethane rich gas stream (98) and a lower liquid propane rich stream (38) .
  • Lower liquid stream (38) is pumped via pump (46) to the upper region of absorber (72) .
  • the upper gas stream (98) passes through heat exchanger (84) to cool feed stream (78) and then is combined through a tee (100) with upper gas stream (36) from reflux separator (86) .
  • a typical example of process (70) would be as follows with the specified temperatures and pressures representing approximations of a simulated model.
  • Natural gas feed (12) enters process (70) at a temperature of about 86°F at a pressure of about 612 psia.
  • the upper portion (82) is split into streams (76) , (78) and (80) which are cooled to about 71°F.
  • the lower portion (86) is cooled to about -40°F with a pressure of about 609 psia.
  • Stream (78) is further cooled to about -112°F with a pressure of about 606 psia.
  • Stream (80) flows directly to absorber (72) .
  • Streams (76) and (78) are cooled respectively to about -70°F and -112°F and flow to absorber (72) .
  • Bottom liquid product (20) exits absorber (72) at a temperature of about -38°F and a pressure of about 606 psia.
  • Upper gas stream (22) exits absorber (72) at a temperature of about -99°F and about 605 psia.
  • stream (32) is at a temperature of about -122°F and a pressure of about 413 psia.
  • Gas stream (98) is at a temperature of about -122°F and 413 psia exiting reflux separator (96) .
  • stream (98) After passing heat exchanger (84) , the temperature of stream (98) is warmed to about -88°F and is about 408 psia.
  • Stream (98) is combined with upper gas stream (36) from reflux separator (86) .
  • the combined stream is at a temperature of about -87°F and a pressure of about 408 psia.
  • the combined stream is warmed in heat exchanger (16A) to a temperature of about 78°F with a pressure of about 403 psia.
  • the stream is warmed in heat exchanger (40) to a temperature of about 86°F and a pressure of about 628 psia whereafter it is compressed in compressors (42) and (48) , cooled in air cooler (60) and heat exchanger (40) , and exits the process as a residue gas stream (44) which consists predominantly of methane and ethane.
  • Lower liquids stream (20) is warmed in heat exchanger (18) , and enters the deethanizer (24) at a temperature of about -66°F and a pressure of about 416 psia.
  • the upper gas stream (52) exiting deethanizer (24) is at a temperature of about 12°F and a pressure of about 413 psia.
  • the lower liquid stream which is the NGL product stream containing the propane, butane and like fractions is at a temperature of about 195°F and a pressure of about 416 psia.
  • Reflux separator (86) receives the upper stream (52) at a temperature of about -34°F and a pressure of about 408 psia. This stream is separated into an upper gas stream (36) and a lower liquid stream (90) at about the same pressure and temperatures .
  • FIG. 3 there is shown still another embodiment of the present invention where like numerals designate like or similar features.
  • the system and process (110) shown in Fig. 3 obtains a very high propane recovery of about 99.2%.
  • Fig. 3 is similar to Figs. 1 and 2 except that reflux separator (96) has been replaced with an additional absorber (114) .
  • Absorber (114) receives liquid/gas stream
  • Absorber (114) also receives upper gas stream (36) from reflux separator (86) .
  • Upper gas stream (36) passes through heat exchanger (116) where it is cooled and partially condensed prior to entering the upper region of absorber (114) .
  • Absorber (114) operates in a manner similar to absorbers (14) and (72) , and may contain either packing, trays, or other contacting means.
  • the upper gas stream (118) from absorber (114) is warmed in heat exchangers (84) and (16A) where it first cools feed stream (78) , and then (76) , (78) , and (80) respectively. It then flows in a similar path to that described with reference to Fig. 2.
  • the temperature and pressures provided for Fig. 2 are approximately the same for Fig. 3.
  • the absorber (114) receives liquid-gas stream (32) at a temperature of about -120°F as compared with -122°F for the liquid/gas stream (32) entering reflux separator (96) in Fig
  • the absorbers (14) , (72) , (114) may be any contacting device operating in the manner described.
  • other modifications including addition or substitution of equivalent structures may be made to the system. Referring to Fig. 1, one such modification could be to insert a separator in which streams (50) and (12) combine upstream of absorber (14) .
  • a dephlagmator (refluxing heat exchanger) could be installed above the separator.
  • Stream (36) could cool the dephlagmator.
  • expander (30) may be any expansion means such as a turbo-expander, two turbo-expanders operating in series, or a Joule-Thompson expansion valve.
  • the number of stages or trays in absorbers (72, 114) depends on the inlet composition of the feed gas and other factors including process economics.

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Abstract

Selon l'invention, on augmente la récupération de propane, butane et autres constituants plus lourds, à l'intérieur d'un flux de gaz naturel, en installant un absorbeur en amont d'un dispositif d'expansion et d'un séparateur. Ce séparateur est situé en aval du dispositif d'expansion et il renvoie vers l'absorbeur le flux liquide produit par le séparateur. En outre, on augmente la récupération de propane, butane et autres constituants plus lourds en combinant le flux de gaz supérieur provenant d'une colonne de distillation avec le flux de gaz supérieur provenant de l'absorbeur, préalablement à l'injection de cette combinaison dans le séparateur. Ensuite, on traite le flux de gaz supérieur enlevé du séparateur, afin de récupérer un flux gazeux à dominante méthane et éthane, tandis que l'on distille ultérieurement le flux liquide inférieur provenant de l'absorbeur, afin de produire un flux composé principalement de propane, butane et autres constituants hydrocarbures lourds. D'autres modes de réalisation comprennent l'ajout dans le système d'un séparateur additionnel de reflux, ou le remplacement du séparateur par un absorbeur supplémentaire.
PCT/IB1996/001249 1995-11-03 1996-11-01 Procede de recuperation de propane WO1997016505A1 (fr)

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GB9807591A GB2323605B (en) 1995-11-03 1996-11-01 Propane recovery process
CA002235883A CA2235883C (fr) 1995-11-03 1996-11-01 Procede de recuperation de propane
AU73296/96A AU7329696A (en) 1995-11-03 1996-11-01 Propane recovery process

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AU7329696A (en) 1997-05-22
CA2235883A1 (fr) 1997-05-09
GB2323605B (en) 1999-04-07
CA2235883C (fr) 2001-08-21
US5685170A (en) 1997-11-11
GB9807591D0 (en) 1998-06-10
GB2323605A (en) 1998-09-30

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